Figure captions:
Figure1. The sequence of cyclic process
Figure2. The thermodynamic diagrams for the system in terms of
(a) x-y diagram and (b) ternary and residue curve map
Figure3. Comparison between experimental data and model for (a)
diethyl ether and (b) ethanol for feed flow rate of 333 kmol/h
Figure4. Out-put of model in terms of (a) concentration of
ethanol and diethyl ether as a function of time, (b) time interval of
27000 s for concentration of ethanol and diethyl ether as a function of
adsorbent length and (c) temperature profile variation versus time at
different length of bed for feed flow rate of 333 kmol/h
Figure5. Variation in (a) the Peclet number, (b) the Reynolds
number, (c) maximum superficial velocity and (d) minimum fluidization
velocity with timefor feed flow rate of 333 kmol/h
Figure6. Reaching to cyclic steady state condition for (a)
ethanol and diethyl ether profiles, (b) water (steam) distribution and
(c) temperature profile with time for feed flow rate of 333 kmol/h
Figure7. The average contribution of utilities cost from total
operating costs
Figure 8. Interaction between parameters in terms of (a) A×C
(for diethyl ether cyclic recovery), (b) A×D (for diethyl ether cyclic
recovery), (c) B×C (for diethyl ether cyclic recovery), (d) D×C (for
ethanol cyclic recovery), (e) B×C (for ethanol cyclic recovery), (f) A×B
(for total operating), (g) A×C (for total operating), (h) B×C (for total
operating)
Figure 9. The optimization path